Method and apparatus for treating compounds preferably of a hydrocarbon nature



May 28, 1929. w, 1 KNOX 1,715,239

METHOD AND APPARATUS FOR TREATING COMPOUNDS PREFERABLY OF A HYDROGARBON NATURE May 28, 1929. wI J; KNOX 1,715,239

METHOD AND APPARATUS FOR TREATING COMPOUNDS PREFERABLY OF A HYDROCARBON NATURE Original Filed Sept. 9. 1922 3 Sheets-Sheet 2 9/ INVENToR. i W/LL Mw ./abw /f/vax ATTORNEY May 28, 1929. w, J, KNOX 1,715,239

METHOD AND APPARATUS FOR TREATING COMPOUNDS PREFERABLY 0F A HYDROCARBON NATURE O rignal Filed Sept; 9. 1922 3 Sheets-Sheet 5 Patented May 28, 1929.

UNITED STATES PATENT OFFICE.-

WILLIAM JOHN KNOX, OFNEW YORK, LN'. Y., ASSIGNOR, BY MESNE ASSIGNMENTS, TO

PETROLEUM CONVERSION CORPORATION, A CORPORATION OF DELAWARE.

METHOD AND APPARATUS Fon TREATiNG COMPOUNDS PREFERABLY or A HYDRO- CARBON NATURE.

Application filed September 9, 1922, Serial No. 587,191, and in Canada August 24, 1922. Renewed April 16, 1929.

v My invention relates to a new and useful method and apparatus for treating compounds preferably of a hydrocarbon nature, in order to produce therefrom, or to recover therefrom, constituents' having commercial Zuse or application, and the inventionparticularly contemplates the treatment or conversion of hydrocarbons to form other desired hydrocarbon combinations or compounds. l

My invention is an improvement over that disclosed in my co-pending application filed I v March 24, 1919, Serial No. 284,818, now Patent' No. 1,428,641, issued September 12, 1922. In this patent a process of cracking or converting oils was disclosed in which the oil to be cracked was fed as liquidto a container constituting a -reaction chamber, and the heat for cracking such oil was furnished -by` means of a heated gas, of hydrocarbon origin,.which was introduced into such chamber. In contradistinction to such process, the present invention vcontemplates introducing into the reaction chamber, separately from any liquid oil which isA introduced, `quantities of oil vapors which when condensed are too heavy to be suitablev as motor greatly extended surfaces, thus facilitating` fuels. These vapors, which in the preferred embodiment may previously have been heat edto' incipient cracking, are physically contacted with the heated gas which performs the function of a heat-carrier, andare there'- by cracked, it having been found that such conditions are fav`orable to the production of a motor fuel of a high value. A further feature of the invention consists in causing any oil, introduced into the reaction chamber as liquid, to flow in thin films over the heating and vapol'izing thereof by contact with the heat-carrier gas.

- A. further vand important feature of theA thereto the' invention resides inthe manner of heating the carrier gas by regenerative heating means, which in the disclosed embodiment consists of, a brick-filled hot blast stove, similar to that used in iron smelting, con.-

taining a multiplicity of lues. Tolthe best of my knowledge this is distinctly new to the art.- By this means, large quantities of heat are stored with high efficiency by burning liquid or gaseous fuel and this heat is siderable period of time in a steady, uniform manner and carried into direct contact with large surfaces of preheated Oil and hot'4 vapors.

Other objects of'my invention will appear in the specification and will be particularly pointed out'in the claims.'

In the accompanying drawings tobe taken as a part of this specification, I have fully and clearly illustrated an apparatus which is constructed in accordance with my invention,and whichA is particularly adapted for carrying out my improved process, but I desire it understood that my invention is not limited to the apparatus illustrated, as the same may be carried out by other apparatus, without departing from the spirit and scope of my invention.

In the drawings,Figure 1 is a partial diagrammatic view, largely in section, show-V ing a complete apparatus or cyclic unit adapted to carry out niy new process. For simplicity of illustration, one hot stove only is shown as a part of the cycle; additional stoves are preferably provided, however, as shown in Fig. 2; Fig. 2 is a side view, partly in section, of a group of stoves and the primary cracking chamber, with pipe connections, valves and temperature-controlling means; Fig. 3 is a cross-section on line III-III of. 4F ig. 2 through oneV of the stoves with plan view of the connecting pipes and operating valves; Fig. 4 is a vertical section of one of the gas-operated lift pumps employed for elevating the pil; Fig. 5 is a cross-section of the primary cracking chamber taken immediately above the vapor inlet showing the vapor pipe for conducting vapors from the evaporating chambers; Fig.. 6 is a vertical section through the evaporating units, with oil and vapor pipes, oil level-regulating device and gas-pressure lift pumps, and Fig. 7 is a detail on a larger ,scale of the'level-regulatf ing deviceshown in Fig. 6.

Like reference characters indicate like parts in the different views.

My invent-ion involves apparatus constitutchamber '64 in the ing a cycle as follows: A brick-filled stove 1, a primary "cracking chamber 2', secondary cracking chamber 2", evaporator 3', evaporator 3 reflux condensing column 4', rectifying column 4", dephlegmating condenser 5, final condenser 6, gasoline accumulator tank 7, which is in gas pipe connection with compressor 44,- which is in connection with the cold end of stove 1. The hot end of the stove is in pipe connection with the primary cracking cylinder 2', and the succeeding parts mentioned above are in serial pipe connection, thus completing the cycle. My invention also includes means for producing a separate vapor cycle, and comprises the Connections 93 and 65 from the vapor cha-1nbers of the evaporators 3', 3, to the upper primary cracking cylinder 2'.

In order that the invention may be clearly understood; the several parts of the apparatus above enumerated and others necessary to the performance of my invention will now be described in detail.

Heating elements or stoves.

Each of the stoves illustrated in Fig. 2 is preferablyof the type known as a twopass stove. Each stove is provided with a valved burner inlet 47- through which liquid or gaseous fuel is admitted to the combustion chamber or hot end shown in stove 1".- A cold gas main 45 leads from the circulating; compressor (hereinafter described) to the stoves and a hotgas main 51 leads from the stoves to the top of the cracking chamber 2'.` To heat the stoves, the valves 49 in the cold gas pipe 45 and the valves 50 in the hot gas main 5l, are first .closed to cut the stove out of connection with the system, chimney valve 52 is opened and fuel and air are admitted through the inlet 47. Combustion takes place in chamber 48 and in the central flue 53. the flames pass upward to the dome of' the stove and thence downwardly through a multiplicity of vert-ical fines surrounding the central flue, as illustratcd in the stove at the left of Fig. 2.

Heat is imparted to the brick or other heat.

storage device and stored therein in this manner and the final products of combustion pass through the stack valve 52 to the chimney. vIn operation, one. of the stoves is cut into the system and employed to heat the circulating gas and transmit heat. to the cycle, while the remaining two stoves are' cutout of the system and heated up, the time period for heating up thus being approximately twice that of the running period.

The method of' operating the stoves consists in first charging n. stove which has been'` heated up to its Working temperature with oil gas or residue gas and bringing the gas pressure therein up to the Working-pressure of the system. For example, when stove l is in operation in the system and stove 1' has been prepared to be cut'. in as above, valves 49 and 50 'on stove 1' are opened and the circulating gas passes momentarily through both' stoves 1 and 1', then the corresponding valves 49, 50, on stove 1 are closed. There is thus no interruption in the circulation of hot gas to and through the system. v Y

Stove l having been cutout of the system, it will be left full of gas under the pressure of the system, for example, 250 lbs. per square inch.v At the cold end of eachstove, a valved outlet pipe 54 Figure 2 is provided through which the gas stored in the stove is now discharged into gas-holder tank "55, shown in Fig. 1 by means of a suitable con duit not shown, or to other point of storage or utilization. This leaves the gas in the stove at approximately atmospheric pressure. This gas isv now driven out or scavenged by injecting` into the top of the stove a small amount of water through a pipe 56 connected with water under pressure.

The heat radiated from the. brickwork vinstantaneously converts the water into steam which drives out the remaining gas to the holder. Simultaneously with this scavenging operation and the closing of valve 56, the stack valve 52 is opened and burner valve 47 is opened. Firing is then allowed to proceed until the stove is restored to the desired temperature condition.

In order to cut this stove into the system, the burner valve is closed and a small amount of water is injected into the dome of the stove to scavenge the products of colnbustion into thechinmey The chimney valve is then closed and fuel oil or the heavyl residue oil Afrom the system, from the residue oil tank 14, is the stove by means of pipe and valve 57 all of the other valves of the stove being closed. The oil entering the stove is cracked quickly byv the heat radiated from the brickwork and oil gas is `generated. Oil is injected and cracked into oil gas until the pressure guage on the stove indicates the same pressure as that carried in the system itself. The stove is now in condition to be cut into the circlilating system in the manner described above.

The length of time that a stove may be used to deliver heat to the system depends mainly on its size or heat storage capacity and the amount of gas passed through it. During the period of blastior the time. it is in use in thecycle, the temperature of the stove will gradually drop to a predetermined point, at' which point the stove. will be cut out. It is necessary and desirable that the temperature of the hot gas entering the cracking chamber 2' shall be uniform at all times. Means employed for maintaining such uniform gas temperature are shown in Fig. 2.

for example, injected into rinto the hot gas main ,51, the by-pass prefern? peinture in the top of the cracking chamber.

Temperature' control means for crackin-g chambers.

I'have'shown in Figure 2 an extension or by-pass pipe 58 from the cold gas mam 45 ably being provided with a valve 59. 4By this means, cold gas may be admixed with the hot .gas from the stove to modify its temperature and to maintailta consta-nt teni- This may be done. by hand iu connectiiim with a -pyrolncter placed in the top`of the hot gas main, as shown at 90, which affords an indica-tion of the temperature therein, but I preferably intel-pose between the pyroineter and the valve, a pyrometer-controlled power mechanism by means of which the valve 59' is gradually niovedas the temperature tends to change and more or less cold gas blended andadmixed with the hot gas. This pyrometric-power cont-rol and valve is of a well known type andis indicated, generally, in Fig. 2 by the numeral 59a. In this manner, the temperature of the gas entering the cracking chamber is maintained during the whole-period of the run at a uniform point which does not fluctuate in practice more than 25 -F. and may be controlled within a 10 range.

Omo/bring fzhw'ftbe'rs.v

- The primary cracking chamber 2 is shown in Fig. 2 and the complete cracking unit consisting of-two chambers, 2 and 2, is shown in Fig. 1. The primary cracking chamber 2 preferably consists of a vertical cylindrical steel shell connected near the top with hot gas main 51 with an outlet gas and vapor pipe 158- at the bottom connecting it with the bottom of the secondary cracking chamber 2. v The secondary cracking chamber 2 provided with anoutlet gas and vapor pipe or conduit 68 at the top leading to evaporator' 3. These chambers 2 and 2" are preferably lined with heat-resisting refractory walls 159 to prevent the loss-of heat and to protect the steel shells. A metallic grid 6l is preferably placed above the bot toni and above the outlet, which supports a cohnn of. special refractory shapes 60.

These sha es arranrcd 1n la ers and stav- 1 zn gered,- have la-rge surface area for spreading -and filming the oil to'be cracked and spiralled openings for the passage of. the hot gases and to cause the hot gases y to-effectively contact with the films of oil. In the center ofthe primary'cracking cylinder 2 is 'an .extension of the duct pipe' 62 from oil lift j pump '13. This pipe is capped with a spray head or deflccting bonnet 63 which vcauses the oil as it emerges from 62 to be thrown downw'ardly over the top-layer of thelling 60. Above the filling th`ere is -a freespace or ,chamber 64 intowhich the hot gas from the stove, maintained at a uniform temperature by intermingling cold gas therewith, enters from hot gas mainv 51. The object of this gas chamber is to check the velocity of the gas and' to cause it to spread and Contact 70 by vapor pipe 65 to the concentric distribut- '1- ing pipe 66, and vblown' or discharged through several spaced nozzles through aportures in the shell and lining into'the gaschaniber 64.

Chamber 2 is the primary cracking cham'` if' berof the system. As will be pointed out, large quantities of residual Vgas and hydrogen under pressure of the system, for example, 250 pounds per square inch, are heated to a uniform temperature and discharged into the chamber 64. The velocity of said gases is partly arrested and they descend evenly through the chamber-.and column of filling. Hot vapors aile conducted from the' recuper.- ative part of the system after having been U0 generated and trapped in the evaporators and are discharged into chamber 64, below the hot gas stream entering from 51. The hot A gases and vapors'commingle and the latter are heated to a desiredV cracking temperature J5 and the combined gases and vapors pass through the oil spray from the lspray head 63, and pass downwardly through the filling 60 and impart heat to the thin films of oil on the large surfaces. The flow of oil from the educt pipe 62 and spray7 head 63 is maintained preferably at such, a rate as to keep the tile surfaces .wet at all times. The vola-,- tile portions of the oil on the large surfaces are evaporated and the descending hot gases and vapors commingle with the freshly generated 'vapors and impart the desired temperature to the latter and.- cause them tocrack. 'The resulting vapors 'and heated gas pass out through conduit 158 into the Abottom 110 of the secondary cracking chamber 2.A

The secondary cracking chamber 2" is similar in regard vto shape and refractory, heatinsulating lining to 2 lbut its-interior lcontains only-the special tile filling 60and gas-vapor spaces at top and bottom respectively. The purpose of this secondary crack- 'ing chamber is to retard and hold wet oil spray and inist mechanically carried by the -gas stream and to thereby afford further l heating and cracking action. "Another pur-I pose served by this chamber is to more com# pletelycomniingle the hot gases and vapors and to furnish space and time for recombinanation into saturated products. l

The tile filling used in the cracking chambers and in the other vessels serves also as an efiicient thermal stabilizer. Whenthe system is under normal operating conditions,

the heavy mass of the tile will have absorbed 13' oil from evaporator 3 to evaporator 3 for the purpose of insuring a level of oil in equilibrium in the two vessels whether the lift 12 is in operative condition or not. Another function served by pipes 30 and 31 is to allow oil to flow back into lift- 12 and a. forced rapid recirculation of the oil can thus be obtained so as to securel the advantages of rapid circulation of oil through the tubes and a greater or more efficient heat "L transfer. By means of pipe 32 connecting evaporator 3 to the bottom of lift 13, oil flows by gravity into the lift and is lifted by pressure gas to the top of cracking chamber 2 and sprayed over the tile surface therein. As this oil evaporates and more oil f is pumped to maintain the flow over the surfaces, the oil level inthe evaporators tends `to fall and more oil iscaused to flow into oil lift 11 and to be raised and discharged vinto evaporator 3, asirequired, by the operation of the level-regulating device 106 and valve 28.

Recz'fyng and con-lensing apparatus.

heati exchanger 69 in evaporator 3 and pass upwardly through the column of filling contacting` with the oil flowing downwardly therethrough, Which is being continuously pumped and discharged into the top by oil lift pump 10.

Rectifying column 4 is of similar general construction to 4; that is, a vertical steel shell connected by pipe 74 with top of the refluxcondensing column 4 to conduct the gas and vapors therefrom and extended tothe bottom of the filling so as to.

cause the gases and vapors to pass upwardly through the openings in the.filling and contact with the films of oil flowing downwa-rdly. Above the oil discharge point is an additional section of refractory filling-75 whose object is to retard and retain any mechanicallyl carried'rain or oil mist.

A dephlegmating or reflux condenser 5 is placed ata point preferablyhigh enough to allow fractions condensed therein to run of oil lift pump compressor 33.

back into rectifying column 4 by Way of trap 77 and pipe connection 7 8. The gases and vapors are conducted from the top of rectifying column 4 by pipe 89 to dephlegmating condenser 5. The heavy ends condensed therein run, as described, back into column 4 and the gas and vapors of the desired product pass into a final condenser 6, thence into a suitable tank 7 in which the liquid .product accumulates, allowing the residue'gas to separateand pass to the lcirculating compressor 44 by means of pipe 6. f Uzfrculat'nig apparatus.

The oil lift pumps 'illustrated in detail in Fig. 4 are preferably operated by means of gas from the system. 'As reflux-condensing column 4 and rectifying column 4 are parts of the condensing system and as the gas used in these oil lifts passes directly t0 the water-cooled condensers, unheated gas is hereemployed.' Vhcn the fresh oil in the system and` the reflux oil reaches lift l1, it is above 350o F. and as the gas used in 4the evaporator lifts travels with the evolved vapors to the top of the primary cracking cylinder, I, therefore, preferably employ a tubular superheat-er 36 to heat the gas used in lift pumps 11, 12 and 13. In this manner, the oil heated by the countercurrent flow isnot deprived of any of the heat it .has picked up but additional heatris added to it. As the superheater is not a part of this invention, `it will not be described in detail. l-t is heated preferably as shown by waste products of combustion stoves.

The operation of the o il lift pumps requires the use of gas under suiiicient pressure above the pressure of the system to overcome the vertical head of oil in educt pipefrom the 62. Compressor 44, which, it will be seen, i

is in the cycle, is employedto circulate residue gas from the condensers through the stove and chain of apparatus. The outgoing` gas from this compressor 44 is atthe highest pressure of the cycle. Pipe 46 conducts a portion of this gas to the inlet side The work done by the compressor 33, is measured by the head of oil to be overcome lifts.

passes by means of pipes 34 and 38 to lifts 9 and Al0. By closing valves 35 and 37 and opening' valve 34'., lifts 13, 12 and 11 may be operated through pipe connections 39', 39 and' valve A40, cold gas being used and the superheater by-passed. It is preferable, however, to open valve 35 in pipe connec-Y tion 35 to the superheater, open valve 37 and close 34. Gas from gas main 34 then passes through the superheater and out through pipe 37 to pipe 39 and thence, as above, to lift pumps 13, 12 and 11.

llO

The oil lift pump gas 4from compressor 33 The method of controlling the feed of oi-l to the evaporators by means of a level regulater 106 has been described above. r1`he pivoted Weighted lever 41 employed in this connection for operating the oil inlet valve 28 is also employed to operate the gas inlet valve 40 through connection 43. By suitable adjustment, it will be seen that pressure gas to lift pump 11 will be diminished or entirely cut oiff simultaneously with the action of the oil valve 28 and will open in like manner as valve 28 opens, thus adjusting the gas fiow to the oil feed requirement.

lhe purpose served by the continuous connecting pipes 18, 18".`\18u is to insure a steady uniform head of oil to all the lifts 9, l and 11 and to allow the leveling back of any excess of oil from the vessels 4 and 4 into the feed tank. For example, if lift 9 should fail to operate, the oil flows Without interruption into lift 10. Also, if lift 10 should be allowed to sto the oil from the surfaces in 4 in excess of) feed requirements will run by into feed tanks 8', 8". In other Words, although the normal flow of oil is maintained by the lifts in the direction away from the feed tanks, any irregularities that might result from improper regulation or shutdown of any part are taken care of by the leveling action through pipes 18, 18 and 18.

I do not confine myself to the use of gasoperated lift pumps, but may use reciprocating or other mechanical pumping devices for elevating the oil.

Mode of operation.

In the preferred procedure,l I ma treat a heavy distillate from petroleum oi in order to produce therefrom lower boiling products, such as gasoline or motor spirits. To this end, the system havin been placed under pressure in a manner .to be more full described, one of the oil feed tanks 8 is eut out of the system by closing the valve in pipe 16, which connects its interior with the gas pressure o'f the system, closing valve 17 in oil feed pipe 18, relieving the pressure within tank 8 by opening valve 21 in pipe 22 and opening valve 19 in feed pipe 20 which connects with an external supply of oil. 'Pipe 22 leads to residue gas tank 23 which is in direct connection with the inlet of the compressor 24 and with the residue gas holder 55. Oil will now flow into feed tank 8l by suction or gravity or may be forced in by means of a pump in line 20. By restoring valves 15 and 17 to their original positions, feed tanks 8 and 8 will both be under the pressure of the system by means of the connection through pipe 16 and both will will be in liquid connection with the oil lift pump 9.. The oil feed tanks 8, 8 are now in operative connection with the system and oil will iow into the oil lifts 9,

10 and 11 by gravity through pipe 18 and its extensions 18 and 18".

' rlhe oil is forced by means of oil lift pump 9 into the upper part of rectifying column 4 and is discharged on the top layerI of the main column of filling. This oil, together with the condensate from dephlegmating or reflux condenser 5, meets the vapors and gases from-reflux-condensing column 4 ad-v mitted by pipe 74, these vapors and gases passing in the reverse direction 'to the incoming oil. The oil flowing downwardly over the surfaces in countercurrent direction to the ascending gases and vapors is colder than the latter and, therefore, condens-es out therefrom vapor constituents heavier than the desired final product. These condensed heavy fractions iiow down- Wardly With-the fresh oil through leg 25 into pipe 18 to lift pump 10, which forces it through pipe 100 into reuX-condensing column 4. As in the case of column 4, the oil mingles With gases'and vapors of a higher temperature (the latter having been used'to heat oil in the evaporators 3', 3) and a similar action takes place, the oil becoming hotter and its volume augmented by the condensing and refluxing of the intermediate boiling point vapors in the gas or vapor stream.A From reflux-condensing column 4', the oil passing through pipe 25 and valve 28 is forced by lift pump 11 into the top portion of evaporator 3 where the checkerwork produces further vaporization. The level of oil in the two` evaporators is maintained constant at a point slightly above the tubes 69, as has been described.

Here the oil is heated and .vaporized by the hot vapors and gases from the reaction chamber Which pass in heat exchange relationship to the oil in tubes 69 and under the conditions obtaining in the evaporators y the oil is heated to incipient cracking.

The oil from evaporators 3 and 3 new at a temperature around 700o F., depending upon the character of the hydrocarbon treated and under the pressure prevailing in the system, usually in the neighborhood of 250 32 into oil lift 13 by means of which it is forced into the reaction chamber, preferably in the form of a spray, as shown, and flows over the extended tile surfaces in thin films.

Previous to this, a stoverin the system has been heated up. Gases from the system as, forl'example, from residue gas tank 55, or hydrocarbon gases from an external source, if desired, are forced by means lof compressor 24 and compressor 44 into the stove through pipe 45. The temperature of the stove is sutlieient to impart to the gases. an average temperature in the neighborhood of 1400? F. .in order that the heat-bearing gases may maintain in the reaction chamber 2', a temperature between 1150 to 12000 F. which,

4pounds per square inch, passes through pipe in general, has been found to beV the preferable temperature range. It will be understood, however', that time as well as temperature is a factorin the cracking of oils so that if a very high temperature is to be employed then the time factor mustbe very 'short and vice versa.

4been described. I

It will now be seen that hot oil is caused to pass over greatly 'extended surfaces in the reaction chamber and is in a most favorable condition, for the action of the hot gases and vapors from the stove maintained at the optimum temperature and pressure. The gases' from the stove contain a large proportion of hydrogen and, due to the favorable reaction conditions maintained in the chamber, the formation of unsaturated c ompounds can be minimized.

The vapors evolved in. the evaporators, being as a rule too heavy for use as motor. spirit, are normally led through pipes- 93 and into the reaction chamber. Thus the etroleum entering the reaction chamber has een separated-into two portions; that which could be vaporized under the condi-- tions obtaining in' the evaporating system is admitted as such at 64, Whereas the liquid portion admitted Hows in thin films over greatly extended surfaces, both portions thusv being in the most favorable condition for cracking. v

.ln case it is desired to replenish the supply of fixed gases in the system,- a portion, or the Whole of the vapors produced in evapoiatoi-s 3 and 3, may beadn'iitted to pipe 45 by Amanipulating valves 86 and 87.

-The liquid residue from'chambers2 and 2" is allowed to pass into' the sump 14 through pipe 14 whence it may be recirculated by means of lift 13 and 'pipe 14, or t may-be drawn off to a point of storage or utilization by means of valve 141 at the bottom.

The vaporsand gases from reaction chamber 2' now pass into chamber 2" where addi-- tional extended surfaces are presented. The function of the secondary .cracking chamber has already been described. -The h'ot products from the secondaryreaction chamber 2 pass around tubes 69 in evaporators 3. and 3 and afford the -heating nieans therefor. The condensate from the gas andfivapor stream refiuxedjn the heating .spacesof the mary.` crackingv chamber.

evaporators 3 and 3 Hows out through pipe 92 into lift pump A11 whence it is returned to the vapor space of the evaporator 3. i i

The vapors and. gases having yielded a portion of their heat in the evaporators pass therefrom through 72 into the reflux-condensinn column 4 and thence into rectif ino' b D column 4", as has been described. The uncondensed portions then pass through reflux condenser 5,'and condenser 6, the condensate being' collected in tank 7. This condensate represents the final liquid product of the system.

As shown above, the vapors in the gasvapor stream from the .primary cracking chamber 2, in passing through the train. of apparatus toward the final condenser 6, pass through a. descending scale of temperatures produced bythe counter o'W of the 'colder oil toward the cracking chamber. A large portion of the vapors generated in cracking chamber 2 are heavier in boiling point than` the desiredproduct and these heavier 4vapors are condensed by the lowered temperatures, join the oil stream and are continuously returned to the interior of the evaporators..v In the 'evaporators such portions ofthe refluxed fractions thus returned from4 the d'ephlegmating condenser 5, rectifying columnA 4" and Ireflux-condensing column 4, together 'with lower-boiling point fractions produced by the cracking of oil in the heat-exchangers, are to a large extent vaporized and are caused to pass by virtue -of their vapor pressure through pipe connections 93, 65,-into the top of the pri- In this manner not only'is the sensible heat of the va ors and gases conserved but also the latent eat of condensation.- An important -function and advantage of the. system, however, is the continuous condensing out of continuous return of these fractions to and A vapors heavier than the"desired p roduct and the through the cracking chamber.' The condil tions of temperature, pressure'an'd atmosphere in the cracking chamber aremaintained at the most effective points for producing a maximum conversion into'.t e desired product. l

Although I have4 found thatin this proc'-l ess the amount of oil broken down into fixed gases is inconsiderable, there is sufficient gas formation to maintain pressure in the system autogenously. To regulate the pressure and prevent the accumulation 'of pressure above the desired point, -a n outlet 83 and weighted backpressure 'valve 84 are providedl on the accumulator tank 7. V'lhe excess residue gas that may beethus discharged enters ga s-receiving'tank 23, whence any' liquid condensate that may be separated-out is removed through valved connection 85. The residue gas entering4 tank 23 passes by way otpipes 79 and 80 to gas holder stor-v the partial pnessures of the vapors ofthe liquid inthe cracking'chamber are' only a small fraction thereof. The pressure will be greatest in the 'stove and cracking cylinder l'and less in the subsequent units on account i of the fiic'tional resistance ot the gas passing through the system and lowest in` accu.

inulator tank 7 The weighted back-pres sure valve 84 is set to the right point ot pressure so as to allow of the escape of any excessof gas. If 'the `pressure of the plant has been discharged or allowed to become much lowered below the working pressure, oil is injected into the stove through valved connection 57 and cracked into oil gas until the pressure is restored. Any fluctuations in pressure are automatically cared for in a similar manner by connecting an olstorage tank directly with inlet 57 and maintaining a gas pressure on the oil equal to that of the system by a gas-pressure balancing pipe. It, for any reason, the ressure in the system vis allowed to drop, oil will flow through 57 automatically, and by virtue of crackin to oil gas, restore the pressure condition. *or small-iluctiiations, however, ,a small compressor 24, which I. have termed a plenum com ressor, is provided which receives gas by ircct connection with the ioating gasliolder residue 'tank 55 and forces gas into `the cycle, discharging the gas into the cold gas main 45. ,This plenum Compressor 24 is caused to operate by connection, not shown, with the pressure of the' cycle. If-the pressure in the cycle drops below the desired pressure, compressor 24 by the automatic closing of a-valve the by-'pass 82,=draws gas from the storage holderand forces it into the cold gas main 45. By means -ot' these two methods, though either method can be used independently, the pressure of the system can be maintained with a minimum variation independent of the temperature.

. It will be understood that the hydrocarbon `gases passing through the hot blast stoves will be subjected to severecracking and that their composition will tend to approach a mixture of hydrogen and methane of varying proportions. n general, this will betrue regardless of the composition of the hydrocarbon material passe the stoves. The function of these gases is not only to supply heat to' accomplish con-k version of the hydrocarbons, but is considthrough ered to form 'a so-called protege-tive atmosphere which will haveA the effect 'of inhibit- 4ing the formation ot fixed gases from the cracking reaction and thus throw the equilibrium in the direction of the )roduct desircd, as for example gasoline.J )B pression hydrogen containing gases itis meant to include, either singly or collectively hydrogen per se as well as methane and similar gaseous hydrocarbons ot neutral character.

I, claim: f

l. The process of producing hydrocarbon compounds, which consists in `feeding a liquid hydrocarbon into a chamber, heating said liquid l-iydroi-.arbon while in said chamber by contacting heat-cd hydrogen containing gases therewith, subjecting thc-hydrocarbon coming into said chamber to a preliminary partial fractional distillation. bv thermally contacting the heated gases 'and vapors from said chamber therewith and passing the vapors and gases from sai-d fractional distillation directly into said chamber..

2. The process of producing hydrocarbon compounds which consists in teedinr a liquid hydrocarbon into a chamber, heating said liquid hydrocarbon while in said chainber by contacting heated hydrogen containing gases from a heating element therewith,

subjecting the hydrocarbon coming into said chamber to a preliminary partial fractional distillation by thermallyv contacting the heated gases and vapors fromsai chamber therewith and .passing a portion of said vapors to said heating element and a portion to said chamber.

3. The process of producing hydrocarbon compounds, which consist-s in feedinga liquid hydrocarbon into a chamber, heating said liquid hydrocarbon while in said ehambei by contacting eheated cracked hydrocarbon gases and vapors therewith, subjecting the hydrocarbon'- coming into said chamber to a preliminary' partial fractional distillation by thermally contacting the heated gases and vapors from said chamber therewith, passing the vapors and gases from said fractional distillation directly into said chamber and subjecting uncondensedA vapors and gases from 'the chamber to condensation conf ditions, heating the uncondensed vapors and gases and utilizing them to convert additional` quantities of said hydrocarbon.

4. The process of producing hydrocarbon compounds, which consists in feeding a liquid hydrocarbon into a chamber, hea-ting said liquid hydrocarbon while in said chainberb'y contacting heated cracked hydrocarbon gases andl vapors from a heating ele-" ment therewith, subjecting the hydrocarbon coming into said chamber toa4 preliminary partial fractional distillation by thermally contacting the heated ases and vapors from said'chamber therewit i, passing a portion of said vapors to said heating element, a portion to said chamber and subjecting uncondensed vapors and gases from the chamber to condensation conditions and returning uncondensed vapors and gases to the heating element- 5. The process of producing hydrocarbon compounds, which consists in feeding a liquid hydrocarbon into a chamber, heating said liquid hydrocarbon while in said chamber by contacting heated hydrogen containing gases therewith under mechanically maintained pressure of said gases, said gases being heated to a temperature sufficient to evolve vapor from said hydrocarbon, subjecting the hydrocarbon coming into said chamber to a preliminary partial fractional distillation by thermally contacting the heated gases and vapors from said chamber therewith and passing the vapors and gases from said fractional distillation directly into said chamber.

6. The process of producing hydrocarbon compounds, which consists in feeding hydrocarbon liquid and hydorcarbon vapor into a chamber, heating said liquid and vapor hydrocarbon while in said chamber bycontacting and commingling heated hydrogen containing gases therewith of sufficient volume and heat units to accomplish conversion of said hydrocarbon, subjecting the liquid hydrocarbon coming into said chamber to a partial fractional distillation by utilizing the heated gases and vapors from said chamber as a 'heating means therefor, subjecting the incoming hydrocarbon liquid at a point more remote than the-said fractional distillation point to physical contact with said gases and vapors and subjecting the uncondensed gases and vapors to condensation conditions.

7 The process of producing hydrocarbon compounds, which comprises evolving hydrocarbon vapors from hydrocarbon liquid, subjecting a portion of said vapor to heat, contacting said heated vapor and gases produced therefrom with liquid hydrocarbon in a confined space, whereby other hydrocarbons are produced and admitting to said confined space a portion of said first evolved hydrocarbon vapor.

8. The process of producing hydrocarbon compounds, which comprises evolving hydroca'rbon vapors from hydrocarbon liquid, subjecting a portion of said vapors to heat and pressure, contacting said heated vapor and` gases produced thereform with liquid hydrocarbon in a confined space under mechanically maintained pressure of vsaid vapor and gases,- said vapor and gas being heated to a temperature sutlicient to evolve vapor from lsaid hydrocarbon liquid, whereby other hydrocarbons are produced and admitting to said confined space a portion of said first evolved hydrocarbon vapor.`

-ment or said reaction chamber as desired.

10. Inan apparatus for treating hydrocarbon oils, a' heating element, a reaction chamber, means for feeding hot vapors and gases from said heating element to said reaction chamber, means for feeding gas and -`Vapor to said heating element, means for conducting the products from said reaction chamber in heat exchange relationship to incoming oil, whereby a portion thereof is vaporized, means for Aconducting vapor so produced to said heating element or said reaction chamber as desired, and temperaturecontrolled means for admitting coolervapors o r gases to the reaction chamber to maintain a uniform temperature in said reaction chamber.

l1. In an apparatus for treating hydrocarbon oils, a` heating element, a reaction chamber, means for feeding hot vapors and gases from said heating element to said reaction chamber, a sou-roe' of gases or vapors, means for feeding gask and vapor to said heating element, means for conducting the products from said reaction chamber in heat exchange relationship to incoming oil, whereby a portion thereof is vaporized, and temperature-controlled means for admit-ting relatively cold vapors or gases from said source to the stream of hot gases fed to said ,reaction chamber to maintain a uniform temperature in said reaction chamber.

. 12. In an apparatus for treating hydrocarbon oils, a heating element, a reaction chamber, means for feeding hot vapors and gases from said heating element to said reaction chamber', means for feeding gas and vapor to said heating element, means for conducting the products from said reaction chamber in heat exchange'relationship lto incoming oil, whereby a portion thereof is vaporized, means for conducting vapor soproduced to said heating element or said reaction chamber as desired, and means to com` Apress a portion of the gas andvapor so produced and to subject the vsystem to the resulting pressure.

13. In an apparatus for treating hydrocarbon oils, a heat-ing( element, a reaction chamber', means for feeding hoty vapors and gases from said heating element to said reaction chamber, means for feeding gas and vaporto said heating element, means for con#` lducting the products from saidlreaetion carbons, a reaction chamber, means for subjecting hydrocarbons therein to cracking conditions,.an evaporator comprising a vapor and liquid space and a heating space closed from said vapor and liquid space, checkerwork in said vapor space, means for` admitting heated fiuid to the heating space of said evaporator, means for spraying liquid" hydrocarbon over Said cheekerwork, and means for admitting the thus heated oil into the reaction chamber.

22. In an apparatus for treating hydrocai-bons, a reaction chamber, means for-`sub jecting hydrocarbons therein to cracking conditions, an evaporator comprising a vapor and liquid space and a heating space, eX-

ltended-contact surfaces in said vapor space, means for admitting heated lfluid into the heating space of said eva orator, means including pumping means or flowing hydro; 'carbon oil over said extended surfaces, means for recirculating liquid from-said vapor and I liquid s ace over said extended surfaces, and

means or admitting the thus heated oil to vthe reaction chamber.

23. In an apparatus for treating hydrocarbons, a reaction chamber, means for subjecting hydrocarbons therein to cracking conditions, an evaporator comprising a vapor and liquid space and a heating space, eX---\ tended contact surfaces in said vapor space,

means for admitting hot products from said reaction chamber into the heating space of said evaporator, means for flowing hydrocarbon oil oversaid extended contact surfaces, means for adding the material con-A densed in said heating space toliquid under- -going evaporation and for circulating the combined liquids over said extended surfaces, and means for admitting the thus heated oil to the reaction chamber.

24. The process of treating hydrocarbon compounds to obtain other hydrocarbon compounds therefrom,.which consists in introducing into a chamber petroleum compounds to be converted, heating up a mass of heat absorbing material until said material is at the requis`ite temperature, transferring, by means of gases, the heat from said material to said hydrocarbons in said closed chamber to accomplish the conversion thereof, subjecting the said hydrocarbon coming intosaid chamber to a preliminary partial Afractional distillation by thermally contacting the heated ases and va ors from said chamber therewith, and passi the vapors and gases from said fractiona ..distillal tion directly into said chamber.

- 25. The process of producmg hydrocarbon compounds, which consists in feeding' a hydrocarbon fluid to be cracked into a chamber, heatingsaid hydrocarbon while in said chamber by contacting and commingling heated gases therewith of suicient thermal content and'temperature to accomplish-conversion of the said hydrocarbon, subjecting the said hydrocarbon coming into said chamber to a preliminary'partial fractional distillation by thermally contacting the heated -gases and vapors vfrom said chamber therewith, and passing the vapors and gases from said fractional distillation directly into said chamber. 4

26. The process of producing hydrocarbon compounds which consists in feeding a hydrocarbon fluid'to be cracked into a chamchamber by contacting and commin ling l heated, cracked hydrocarbon gases an( vapors therewith of sufficient thermal content 'and temperature to accomplish conversion of the said hydrocarbon, subjecting the said hydrocarbon -coming into` said chamber to a preliminary partial fractional distillation by thermally contacting the heated gases and vapors from said chamber therewith, and passing the vapors andi. gases from said fractional distillation directly into said chamber, subjecting uncondensed vapors and gases from .the chamber to condensing conditions,heating the uncondensed vapors and 'gases and utilizing them to convert additional quantities of said hydrocarbon.

28. The process of treating hydrocarbon compounds which consists in heating hydrocarbon' liquid and evolving vapors there- `fromat one point, feeding the heat-ed hydrocarbon liquid and evolved vapor into a chamber at a second point, converting said hydrocarbon liquid and evolved hydrocarbon vapor in said chamber by contacting and commingling therewith gas heated in a heating element at a third pintand employing said heated gas and dissociated vapor to heat liquid and evolve further vapors at the first point.

29. Theprocess of producing hydrocarbon compounds, which consist-s in feeding hydrocarbon liquid and hydrocarbon vapor into a chamber, contacting and com'mingling therewith gas, hea-ted to a temperature sufficient to convert said hydrocarbons in said chamber, employing the said gas and dissociated vapors to fractionally distill the incoming liquid hydrocarbon at a point bcyond vsaid chamber, lpassing the vaporsand gases from said -fractional distillation directly into said. chamber, and subjecting the incoming hydrocarbon liquid at a oint more remote than the said fractional istillation poii t to physical contact with said gases and vap rs.

30. `{.he process of producing hydrocarbon compel nds which consists in evolving hydiocarbpn vapor from hydrocarbon liquid, heating a gaseous fluid of hydrocarbon nature troni ,a separate source to above the cracking temperature, supplementing. said fhiid undergoing heating by adding thereto a portion of said vapor, admitting said heated mixture and a portion of said first evolved vapor to a confined space containing liquid hydrocarbon. and mechanically maintaining ressure of the vapor and gases at a desirale value, said gaseous heated mixture hav# ing been heated to a temperature suilicicnt to evolve vapor from said hydrocarbon liquid thereby other hydrocarbons are produced. i

3l. In the process of treating petroleum oils to convert them into compounds suitable as motor fuels, the steps which consist in introducing into a chamberpetroleum com pounds' to be converted, heating up a mass of inert, refractory, heat absorbing material until said material is above the temperature required for the conversion reaction, passing a heat-carrier gas thereover whereby to heat said as to above such conversion teniperature, introducing the thus heated gas into said chamber and there physically mingling same with the petroleum com pounds therein, controlling the temperature of the reacting compounds whereby the 'conversion of said petroleum compounds is brought about under substantially uniform temperature conditions, the products from said reaction chamber containing the vapors of the desired compounds of'thc process in addition to the carrier gas, and subjecting t e products from said .chamber to condiltions producing liquefaction of saidv compounds suitable as motor fuels.

32. In the process of heating petroleum oils to convert them into compounds suitable4 as' motor fuels, the steps which consist in introducing into a chamber petroleum compounds to be converted, heating up a. nia-ss of inert, refractory, heat absorbing material until said material is above the temperature require/dior the conversion reaction, passing a heat-carrier gas thereover whereby to. heat said gas to above such conversion temperature, introducing the thus heated gas into. said chamber and .there 'physically mingling saine with the petroleuni therein, said gas being ofsutlicient quan- "tity and heat units as to furnish substan tialiy the entire heat necessary for the contions, the products from sai version reaction, controlling the temperature of the reacting compounds whereby the conversiont of said petroleum compounds is brought about under substantially uniform temperature conditions, the roducts from said reaction chamber containing the vapors of the desired compounds of the process in addition to the added carrier gas, and subjecting the products from said chamber to conditions producing liquefaction of said compounds suitable as motor fuels.

33. In the process of treating petroleum oils to convert them into compounds of lowcrmolecular weight suit-able as motor fuels, the steps which consist in introducing into a`chamber petroleum compounds to be converted, heating up a mass of inert, refractory, heat absorbing material until said material is above that temperature i'equircd for the conversion reaction, passing a heat carrier gas thereover whereby to yheat said gas to above such conversion temperature, introducing the thus heated' gasA into said chamber and there physically mingling same with the petroleum compounds therein,con trolling the temperature of thereacting compounds whereby the conversion of said petroleum compounds is brought about under substantially uniform teni erature condireaction chainber containing the vapors of the desired compounds of the process in additionto the carrier gas, and subjecting said products -from said chamber to conditions producing liquefaction of said compounds suitable as 'motor fuels with the separation of residual gas and using said residual gas to constitute in part at least the carrier gas.

34. In the process of treating 'petroleum oils to con vert them into compounds suitable as motor fuels, the steps which consist in introducing into a chamber petroleum compounds to be converted,heating up a mass of iiicrt, refractory, heat absorbing material until said material is above the temperature required for the conversion reaction, passing a hydrogen-containing, heat-carrier gas thereover whereby to heat said gas to above such conversion temperature, introducing said heated-gas into said chamber wherein it is physically lmingled'with the petroleum compounds undergoing' conversion therein, controlling the temperature of said' reacting compounds whereby the conversion of said petroleum compounds is brought about under substantially uniform conditions, the products from said reaction 'chamber containing the vapors ofthe desired compounds y of the process in addition to the carrier gas, and subjecting the products froinsaid chamber to conditions producing liquefaction of said compounds suitable as motor fuels.

35. In the process of treating hydrocarbon compounds tocoiivert same' into-compounds sutable 'as motor fuels', the 'steps which consist in introducing into a chamber Ihydrocarbon material to be converted, heat ing up a mass of inert, refractory, heat abversion reaction, passing a heat carrier gas thereover whereby to heat said gas to above such conversion temperature, maintaining said gas at a substantially uniform temperature'above the conversion temperature as said'mass cools down, and then introducing said mixture into said chamber and there physically mingling same with the hydrocarbon therein Whereby the conversion of said'hydrocarbon is brought about under substantially uniform temperature conditions, the products from said reaction chamber containing the vapors of the desired compounds of the process in addition to the carrier gas, and subjecting the products from said chamber to conditions producing liquefaction of said compounds suitable as motor fuels.

36. In the process of treating hydrocarbon compounds to convert Same into compounds of lower molecular weight suitable as motor fuels, the steps which consist in introducing into a chamber hydrocarbon material to be converted, heating up a mass of inert, re` fractory, heat absorbing material until said material is above thetemperature required for the conversion reaction, passinga heat carrier gas thereover whereby to heat said gas to above such conversion temperature, adding a var ing uantity of relatively cold gas to said eateil gas as said mass cools down whereby the produced mixture is maintained at a substantially uniform temperature above the conversion temperature, and then introducing said mixture into said chamber and there physically mingling same with the hydrocarbon therein whereby the conversion of said hydrocarbon is brought aboutv under substantially uniform tem erature conditions, the products from sai reaction chamber containing the vapors of the desired compounds of the process in addition to the carrier gas, and subjecting the products from said chamber to conditions producing liquefaction of said compounds suitable as motor fuels.

37. In the process of treating etroleum oils to convert them into compoun s of lower molecular weight suitable as motor fuels, the steps 'which consist in continuously 1ntroducing into a chamber petroleum compounds to be converted, heatin up a mass of inert, refractory, heat absorbmg material until it is above the temperature required for .the conversion reaction, passing a heatl carrier gas thereover' whereby to heat said gas to above such conversion temperature, and then introducing the heated gas from said refractory material into said closed chamber physically toA mm 1e with said petroleum therein to accomp ish the conversion thereof, controlling the temperature of said reacting compounds whereby the co'nversion of said petroleum 1compounds is brought about under substantially uniform conditions, heating up a second mass of inert, refractory, heat absorbing material until it 'is above said temperature required for the conversion reaction, continuing said gas 4heating step until said refractory-mass first mentioned has cooled oli", cutting off the supply of carrier gas thereto, then heating carrier gas by means of said second heated refractory mass, and introducing the so heated gas into said reaction chamber under continued controlled temperature conditions therein, thus continuing the operation of gas heating by means of successive units of heated refractory material whereby a continuous supply of heated carrier gas is produced and said conversion process is substantially continuous.

38. In the process of treating petroleum oils to convert them into compounds suitable as motor fuels, the steps which consist in introducing into 'a -chamber petroleum compounds to be'converted, heatin up a mass of inert, refractory, heat absorbmg material .in a chamberseparate from said cham# ber first mentioned, until said material is above the temperature required for the conversion reaction, passing a heat-carrier gas thereover whereby to' heat said gas to above such conversion temperature, utilizing the thus heated gas to accomplish the conversion of said compounds under substantiall uniform temperature conditions by intro ucing same into said chamber and there physically mingling same with the petroleum compounds therein, the roducts from said reaction chamber containing the vapors of the desired compounds 'of 4the process in addition to the carrier gas, and subjectino` the products from said chamber to conditions producing liquefaction of said compounds suitable as motor fuels.

39. In an apparatus of the character described, a regenerative heating element, means for burning fuel to heat same, means vfor feeding relatively cold, heat-carrier gas to said element, a reaction chamber-separate from said heatino` element, means for admitting h drocarbon compounds into said reaction c amber which are to be subjected to the action of the heated carrier gas, `means for maintaining temperature conditions in said chamber substantially uniform, means for admitting the carrier gas heated in said l a refractory-line from 'said reaction chamber after the reactionhas taken place.

40. In an apparatus of the character described, `a .regenerative heating element, means 'for burning fuel to. heat same, means for feeding relatively cold heat-carrier gas to saidelement, a reaction chamber separate from said heatin element, and comprising chamber', means for admitting hydrocarbon compounds into said reaction chamber which' are to be subjected to the action of heated carrier gas, means for maintaining temperature eonditionsin said chambersubstantially uniform, means for admitting the carrier gas heated in said regenerative heater to. said reaction chamber,

means. afording vapor liquefaction condi- A tlie unYapor-ized liquld, mingling said' vapor tions, and means joining said liduefaction means with said reaction chamber whereby ta recover a desired product-trom said reapton chamber after the reaction has taken p ace.

4.1. The. process of producing-hydrocarbon. com. olinds of lower molecular weight from by rocarbon. liquid by cracking which consists; in heating up. a mass of inert, heat retaining, material until said material is at the requisite temperature, separately vaporizing. the hydrocarbon to. be cracked without substantial cracking thereof, passing a hydrogen containing gas over said mass of heated inert material, introducing the vapor produced by the evaporatng step mentioned into contact with. th thus heated hydrogen containing gas, said gas being ot' such thermal quality both as to temperature and heat units as .to accomplish substantially the entire cracking reaction and constituting substantially the sole: source of heat for said reaction and subjecting the' vapor and gas products of the reaction to condensing con itiOns.

42. The. p-rocess of producing gasoline-like compounds nfrom. petroleum liquid by 'cracking, which consists in heating up a mass of inert, heat-retaining material, until said matenial. is at the requisite temperature, separately vaporizing 'the hydrocarbons. to be.

vcracked Without substantial cracking thereof,

passing. hydrovenrcoutajning gas ower said mass oli heated inert material whereby the gas attains a, temperature in excess of required for cracking, adding a diminllmlg quantity oi relatively cold `gas to said heated ges as said mass cools. down thereby mllnialning theA temperature ofthe mixture substantially uniform, lntroducing tbevipor prodlledb theevaporati ostepmentioned 'into 60111261; with the thus" cated hydrogen containing gas, said gas'mixture being of such thermal quality both as to temperature and heat unitsas to-accomplish substantially the entire cracking, reaction and constituting the .sole source of heat for said reaction,

-a vaporizing zone distinct from said reaction zone, separating the produced 'vapor from converted vapor and carrier-gasto couditions producing liqueiactiou of said compounds suitable as motor fuels.

44;. In the process of treating petroleum Oils t0. convert. them into compounds suitable as motor tuels, the steps which consist. in storing up heat in a gaseous heat-carrier until the same. is above the conversion temperature, admitting said heated. gas to. a 1reaction zone, subjectingr the oil to vaporiziug conditions Without substantial cracking. thereof in a vaporizing zone distinct from said reaction zone, separating the prodlmed' loo vapor from theunvaporized liquid, mingling said'iapor und Sold heated carrier-gas in said reaction Zone to bring about conversion of said vapor, controlling the temperature of there-acting compounds whereby the conversion, of Said petroleum. vapor is brought.

about under such temperature conditions that a converted product 1s had which is of a composition suitable as a'lnotor fuel, said carrier-vas beiner of such uantit and heat u rp (l .Y

units as to furnish the entire heat necessary to convert said? Vapor so mingled therewith. andsubjecti'ng the mixture of the vconverted vapor and carrier-gas to conditions producing liquef'actiou. of' said compounds suitable 115 as motor fuels.,

' f WILLIAM JonN Knox. 

